US5242550A - Process for the separation of butanes and butenes by extractive distillation - Google Patents

Process for the separation of butanes and butenes by extractive distillation Download PDF

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Publication number
US5242550A
US5242550A US07/840,976 US84097692A US5242550A US 5242550 A US5242550 A US 5242550A US 84097692 A US84097692 A US 84097692A US 5242550 A US5242550 A US 5242550A
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column
butenes
solvent
resultant
head
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US07/840,976
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English (en)
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Lionel Asselineau
Paul Mikitenlo
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IFP Energies Nouvelles IFPEN
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IFP Energies Nouvelles IFPEN
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/34—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping with one or more auxiliary substances
    • B01D3/40—Extractive distillation
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C7/00—Purification; Separation; Use of additives
    • C07C7/04—Purification; Separation; Use of additives by distillation
    • C07C7/05—Purification; Separation; Use of additives by distillation with the aid of auxiliary compounds
    • C07C7/08—Purification; Separation; Use of additives by distillation with the aid of auxiliary compounds by extractive distillation

Definitions

  • the invention relates to a process for the separation of butanes and butenes by extractive distillation.
  • butenes are valuable products, it is necessary to separate them from the butanes.
  • the butenes can themselves be separated into 1-butene and 2-butenes, or can be isomerized into isobutene, which is recycled in the MTBE synthesis unit.
  • the butenes can also be dimerized by the Dimersol (registered trademark) process into products usable in gasoline. This dimerization is a process performed by homogeneous catalysis, in which the catalyst is lost. As the efficiency of the catalyst is proportional to its concentration in the charge, a paraffin-free charge leads to considerable catalyst economies. Moreover, the butenes which have not reacted can be recycled if the butanes have previously been removed from the charge.
  • the process according to the invention comprises an extractive distillation stage under pressure, but the solvent regeneration and butene purification stages are performed differently, as will be shown hereinafter.
  • the process for the separation of butanes and butenes according to the invention can be defined, in general terms in that the charge containing the butanes and butenes to be separated is introduced into an extractive distillation column under pressure, where it is contacted with a polar solvent in which the butenes have a higher volatility than the butenes, the distillate passing out at the head consisting essentially of the separated butanes.
  • the residue collected at the bottom and which mainly consists of solvent and butenes, is passed into a pressure column, where the bottom temperature is adjusted in such a way that the desorption of the butenes is not complete, which makes it possible to limit the column bottom temperature and consequently avoid thermal decomposition of the solvent.
  • the solvent passing out at the bottom and which contains a fraction of the butenes is passed into a purification column under a pressure close to atmospheric pressure and whose operation is regulated in such a way that the head vapor, mainly constituted by butenes, also contains a fraction of the solvent, which makes it possible to partly condense it in order to ensure the reflux of the column, avoiding compression at this stage.
  • the vapor distillate is passed, following compression, into a pressure desorption column.
  • the purified solvent passing out at the bottom is recycled to the extractive distillation column.
  • the charge to be treated is generally a catalytic cracking or steam cracking C 4 fraction, from which the 1,3-butadiene has been removed, e.g., by extractive distillation and whose isobutene content may have been reduced, e.g., in a MTBE synthesis unit.
  • the charges in question mainly contain butenes (1-butene, cis 2-butene and trans 2-butene), n-butane, isobutane, isobutene in a small proportion and, in the state of traces, hydrocarbons having 3 to 5 carbon atoms.
  • the charge composition can, e.g., be:
  • the solvent to be used in the process according to the invention can be any selective polar solvent, i.e., in which the butanes have a higher volatility than the butenes.
  • any selective polar solvent i.e., in which the butanes have a higher volatility than the butenes.
  • the charge to be treated is introduced by the line 1 into the extractive distillation column C1 under a pressure of 4 to 10 bars.
  • the extraction solvent at a temperature below its boiling point at the pressure in question, is introduced by the line 2 into the upper part of the column C1.
  • the solvent introduction temperature is, e.g., 50° to 90° C.
  • the solvent flow can be in a weight ratio of 3 to 15 kg/kg with the charge flow.
  • the column C1 e.g., operates with a bottom temperature of 90° to 140° C.
  • the head temperature is 30° to 70° C.
  • the solvent leaving at the head by the line 3 mainly consists of isobutane and n-butane and possibly a little 1-butene and isobutene, as a function of the column setting.
  • a fraction of the distillate is returned as reflux to the column C1 by the line 4.
  • the remainder of the effluent is collected by the line 5 and can, e.g., be passed to the pool C4.
  • the highly butane-depleted column bottom residue is passed by the line 6 to the lower part of the desorption column C2 under a pressure close to that of the column C1.
  • the bottom temperature of the column C2, which is lower than the temperatures at which the solvent starts to deteriorate, is regulated so as to bring about a partial desorption of the butenes. It is, e.g., 150° to 170° C.
  • the head temperature can be 30° to 60° C.
  • the effluent leaving at the head by the line 7 essentially consists of 1-butene and 2-butenes, as well as possibly a small isobutene proportion. It is condensed and partly returned as reflux to column C2 by the line 8. The remainder of the effluent is collected by the line 9.
  • the bottom residue of column C2 passing out via line 10 consists of a solvent flow still containing a fraction of butenes, e.g., 3 to 5% by weight. It is fed to the upper part of the purification column C3 operating at a pressure close to 1 bar (e.g., 0.7 to 1.5 bars) and between a bottom temperature of 140° to 170° C. and a head temperature of 120° to 150° C.
  • the effluent leaving the head of the column C3 by the line 11 is partly condensed.
  • the liquid phase is returned as reflux from the reflux flask B to the column C3 by the line 12.
  • the vapor phase essentially consists of butenes and contains a small proportion (e.g., 3 to 6% by weight) of solvent and is passed by the line 13 to a compressor K, in which it is raised to the pressure of the column C2 before being introduced by the line 14 into the lower part of said column C2.
  • the column bottom residue leaving by the line 15 is substantially pure solvent. It is recycled to the extractive distillation column C1.
  • the thermal energy transported by this solvent flow generally at a temperature of 150° to 170° C., can be partly used for heating the bottom of the column C1 via the exchanger E1 and partly for reheating the charge to its bubble point via the exchanger E2.
  • the solvent flow can be cooled through the exchanger E3 before being passed by the pump P and the line 16 into the column C1.
  • a topping up of solvent can take place by the line 17.
  • butenes with a degree of purity of, e.g., approximately 97% by weight or higher if necessary, mainly as a function of the solvent proportion used and the efficiency (number of trays) of the extractive distillation column.
  • the charge to be treated has the composition given in the second column of the table.
  • the solvent used is anhydrous dimethyl formamide with a purity better than 99.8%.
  • the columns used have the following characteristics:
  • the extractive distillation column C1 is a diameter 50 mm steel column having 100 overflow perforated trays.
  • the desorption column C2 is a diameter 50 mm steel column having 20 overflow perforated trays.
  • the purification column C3 is a diameter 50 mm glass column having 10 overflow perforated trays.
  • the three columns are made adiabatic by a heat loss compensation system for the steel columns and by a thermal insulation for the glass column.
  • the column C1 operates under an average pressure of 5.6 bars and is supplied at the 62nd tray by the charge at 50° C., with a flow rate of 436 g/h, and by solvent from the column C3 at 65° C.
  • the solvent enters at the tenth tray at a rate of 2814 g/h.
  • a distillate reflux representing 930 g/h is supplied to the column head.
  • the flow rate and composition of the head effluent after condensation (distillate) are given in the third column of the table.
  • Column C2 functions at an average pressure of 5.4 bars and is supplied at the 18th tray by the preceding residue and at the 20th tray at 130° C. by 114 g/h of the vapor effluent of the purification column C3 (recycling), previously compressed to 5.5 bars. A distillate reflux of 130 g/h is established. The flow rate and composition of the head effluent after condensation (distillate), as well as those of the residue are given respectively in columns 4 and 5 of the table.
  • the column C3 operates under atmospheric pressure and is supplied at the first tray at 140° C. by the residue of the preceding column. A liquid reflux of 200 g/h is established, resulting from the partial condensation of the head effluent. The vapor fraction of the head effluent is recycled to column C2, as stated hereinbefore. At the bottom of column C3 collection takes place of quasi-pure DMF, which is returned to the column C1.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Analytical Chemistry (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Water Supply & Treatment (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
US07/840,976 1991-02-26 1992-02-26 Process for the separation of butanes and butenes by extractive distillation Expired - Lifetime US5242550A (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FR9102385A FR2673178B1 (fr) 1991-02-26 1991-02-26 Procede de separation de butanes et de butenes par distillation extractive.
FR9102385 1991-02-26

Publications (1)

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US5242550A true US5242550A (en) 1993-09-07

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US (1) US5242550A (de)
EP (1) EP0501848B1 (de)
JP (1) JP3138835B2 (de)
KR (1) KR100198897B1 (de)
CA (1) CA2061860A1 (de)
DE (1) DE69203894T2 (de)
ES (1) ES2078678T3 (de)
FR (1) FR2673178B1 (de)

Cited By (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6337429B1 (en) * 1998-04-27 2002-01-08 Basf Aktiengesellschaft Method for separating a C4-hydrocarbon mixture
US6835287B1 (en) * 1999-10-12 2004-12-28 Nippon Sanso Corporation Apparatus, method for enrichment of the heavy isotope oxygen and production method for heavy oxygen water
WO2012145096A1 (en) * 2011-04-19 2012-10-26 International Innotech Inc. Extractive distillation process for recovering butadiene from c4 hydrocarbon mixtures
WO2014058585A1 (en) * 2012-10-09 2014-04-17 Lummus Technology Inc. Flexible butadiene extraction process
WO2014070447A1 (en) * 2012-10-30 2014-05-08 Lummus Technology Inc. Butadiene extraction process
CN104177213A (zh) * 2013-05-21 2014-12-03 中国石化工程建设有限公司 一种制备异丁烷的系统及方法
CN104177212A (zh) * 2013-05-21 2014-12-03 中国石化工程建设有限公司 一种制备异丁烷的系统及方法
US9266808B2 (en) 2006-11-30 2016-02-23 Basf Se Method for the hydroformylation of olefins
US11780789B2 (en) 2019-12-19 2023-10-10 Sabic Global Technologies B.V. Butadiene heat integration process

Families Citing this family (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2842091B2 (ja) * 1992-09-11 1998-12-24 日本ゼオン株式会社 高純度１−ブテン及び２−ブテンの取得方法
DE102005023549A1 (de) * 2005-05-21 2006-11-23 Oxeno Olefinchemie Gmbh Verfahren zur Oligomerisierung von Butenen
ES2731803T3 (es) * 2012-11-07 2019-11-19 Lummus Technology Inc Extracción selectiva de olefina
CN104276917B (zh) * 2013-07-09 2016-03-16 中国石化工程建设有限公司 一种组合工艺制备异丁烷的系统及方法
CN104276916B (zh) * 2013-07-09 2016-03-16 中国石化工程建设有限公司 一种制备异丁烷的系统及分离方法

Citations (13)

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US3769217A (en) * 1971-04-05 1973-10-30 Union Carbide Corp Extractive destillation with subsequent lower pressure adiabatic vaporization
US3772158A (en) * 1971-03-29 1973-11-13 Shell Oil Co Butadiene recovery process
US3890208A (en) * 1973-08-13 1975-06-17 Petro Tex Chem Corp Extractive distillation with furfurol and acyclic ketone cosolvent
US4038156A (en) * 1976-09-21 1977-07-26 Shell Oil Company Butadiene recovery process
US4057995A (en) * 1975-05-13 1977-11-15 Phillips Petroleum Company Apparatus and method for measuring low boiling component contained in relatively high-boiling liquid
US4162198A (en) * 1977-05-28 1979-07-24 Basf Aktiengesellschaft Separation of a mixture of C4 -hydrocarbons by extractive distillation
US4163697A (en) * 1976-02-27 1979-08-07 Compagnie Francaise De Raffinage Process for obtaining isobutylene of a purity higher than 99.5 weight percent
US4419188A (en) * 1980-06-02 1983-12-06 Mccall Thomas F Thermally coupled extractive distillation process
US4545895A (en) * 1984-02-29 1985-10-08 Phillips Petroleum Company Fractional distillation
US4556461A (en) * 1982-01-22 1985-12-03 Nippon Zeon Co., Ltd. Process for separating highly pure butene-1 or butene-1/isobutene mixture from C4 hydrocarbon fraction
EP0216991A1 (de) * 1985-09-11 1987-04-08 Krupp Koppers GmbH Verfahren zur Trennung von paraffinischen und olefinischen C4-Kohlenwasserstoffen
US4718986A (en) * 1983-07-28 1988-01-12 Snamprogetti, S.P.A. Process for producting high purity butene-1 with a low energy consumption
US4777321A (en) * 1987-04-29 1988-10-11 Mobil Oil Corporation Feedstock preparation and conversion of oxygenates to olefins

Patent Citations (13)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3772158A (en) * 1971-03-29 1973-11-13 Shell Oil Co Butadiene recovery process
US3769217A (en) * 1971-04-05 1973-10-30 Union Carbide Corp Extractive destillation with subsequent lower pressure adiabatic vaporization
US3890208A (en) * 1973-08-13 1975-06-17 Petro Tex Chem Corp Extractive distillation with furfurol and acyclic ketone cosolvent
US4057995A (en) * 1975-05-13 1977-11-15 Phillips Petroleum Company Apparatus and method for measuring low boiling component contained in relatively high-boiling liquid
US4163697A (en) * 1976-02-27 1979-08-07 Compagnie Francaise De Raffinage Process for obtaining isobutylene of a purity higher than 99.5 weight percent
US4038156A (en) * 1976-09-21 1977-07-26 Shell Oil Company Butadiene recovery process
US4162198A (en) * 1977-05-28 1979-07-24 Basf Aktiengesellschaft Separation of a mixture of C4 -hydrocarbons by extractive distillation
US4419188A (en) * 1980-06-02 1983-12-06 Mccall Thomas F Thermally coupled extractive distillation process
US4556461A (en) * 1982-01-22 1985-12-03 Nippon Zeon Co., Ltd. Process for separating highly pure butene-1 or butene-1/isobutene mixture from C4 hydrocarbon fraction
US4718986A (en) * 1983-07-28 1988-01-12 Snamprogetti, S.P.A. Process for producting high purity butene-1 with a low energy consumption
US4545895A (en) * 1984-02-29 1985-10-08 Phillips Petroleum Company Fractional distillation
EP0216991A1 (de) * 1985-09-11 1987-04-08 Krupp Koppers GmbH Verfahren zur Trennung von paraffinischen und olefinischen C4-Kohlenwasserstoffen
US4777321A (en) * 1987-04-29 1988-10-11 Mobil Oil Corporation Feedstock preparation and conversion of oxygenates to olefins

Non-Patent Citations (2)

* Cited by examiner, † Cited by third party
Title
S. Ogura, T. Onda, Advances in C 4 Hydrocarbon Processing AICHE 1987 Summer National Meeting, Aug. 16 19, 1987. *
S. Ogura, T. Onda, Advances in C4 Hydrocarbon Processing AICHE 1987 Summer National Meeting, Aug. 16-19, 1987.

Cited By (20)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6337429B1 (en) * 1998-04-27 2002-01-08 Basf Aktiengesellschaft Method for separating a C4-hydrocarbon mixture
US6835287B1 (en) * 1999-10-12 2004-12-28 Nippon Sanso Corporation Apparatus, method for enrichment of the heavy isotope oxygen and production method for heavy oxygen water
US20050129592A1 (en) * 1999-10-12 2005-06-16 Nippon Sanos Corporation Apparatus, method for enrichment of the heavy isotopes of oxygen and production method for heavy oxygen water
US7393447B2 (en) 1999-10-12 2008-07-01 Taiyo Nippon Sanso Corporation Apparatus, method for enrichment of the heavy isotopes of oxygen and production method for heavy oxygen water
US9266808B2 (en) 2006-11-30 2016-02-23 Basf Se Method for the hydroformylation of olefins
WO2012145096A1 (en) * 2011-04-19 2012-10-26 International Innotech Inc. Extractive distillation process for recovering butadiene from c4 hydrocarbon mixtures
US9611195B2 (en) 2012-10-09 2017-04-04 Lummus Technology Inc. Flexible butadiene extraction process
WO2014058585A1 (en) * 2012-10-09 2014-04-17 Lummus Technology Inc. Flexible butadiene extraction process
CN104837796B (zh) * 2012-10-09 2018-11-09 鲁姆斯科技公司 灵活的丁二烯提取方法
CN104837796A (zh) * 2012-10-09 2015-08-12 鲁姆斯科技公司 灵活的丁二烯提取方法
WO2014070447A1 (en) * 2012-10-30 2014-05-08 Lummus Technology Inc. Butadiene extraction process
US9296667B2 (en) 2012-10-30 2016-03-29 Lummus Technology Inc. Butadiene extraction process
CN104903279A (zh) * 2012-10-30 2015-09-09 鲁姆斯科技公司 丁二烯提取方法
CN104903279B (zh) * 2012-10-30 2017-05-10 鲁姆斯科技公司 丁二烯提取方法
US9744475B2 (en) 2012-10-30 2017-08-29 Lummus Technology Inc. Butadiene extraction process
CN104177213B (zh) * 2013-05-21 2016-01-13 中国石化工程建设有限公司 一种制备异丁烷的系统及方法
CN104177212B (zh) * 2013-05-21 2016-01-13 中国石化工程建设有限公司 一种制备异丁烷的系统及方法
CN104177213A (zh) * 2013-05-21 2014-12-03 中国石化工程建设有限公司 一种制备异丁烷的系统及方法
CN104177212A (zh) * 2013-05-21 2014-12-03 中国石化工程建设有限公司 一种制备异丁烷的系统及方法
US11780789B2 (en) 2019-12-19 2023-10-10 Sabic Global Technologies B.V. Butadiene heat integration process

Also Published As

Publication number Publication date
DE69203894T2 (de) 1995-12-07
JPH04312536A (ja) 1992-11-04
JP3138835B2 (ja) 2001-02-26
KR100198897B1 (ko) 1999-06-15
EP0501848A1 (de) 1992-09-02
ES2078678T3 (es) 1995-12-16
CA2061860A1 (fr) 1992-08-27
KR920016120A (ko) 1992-09-24
DE69203894D1 (de) 1995-09-14
EP0501848B1 (de) 1995-08-09
FR2673178A1 (fr) 1992-08-28
FR2673178B1 (fr) 1994-02-11

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